Classifications

• • C—CHEMISTRY; METALLURGY
  • C01—INORGANIC CHEMISTRY
  • C01G—COMPOUNDS CONTAINING METALS NOT COVERED BY SUBCLASSES C01D OR C01F
  • C01G49/00—Compounds of iron
  • C01G49/14—Sulfates
• • C—CHEMISTRY; METALLURGY
  • C01—INORGANIC CHEMISTRY
  • C01G—COMPOUNDS CONTAINING METALS NOT COVERED BY SUBCLASSES C01D OR C01F
  • C01G23/00—Compounds of titanium
  • C01G23/008—Titanium- and titanyl sulfate
• • C—CHEMISTRY; METALLURGY
  • C01—INORGANIC CHEMISTRY
  • C01G—COMPOUNDS CONTAINING METALS NOT COVERED BY SUBCLASSES C01D OR C01F
  • C01G23/00—Compounds of titanium
  • C01G23/04—Oxides; Hydroxides
  • C01G23/047—Titanium dioxide
  • C01G23/053—Producing by wet processes, e.g. hydrolysing titanium salts
  • C01G23/0532—Producing by wet processes, e.g. hydrolysing titanium salts by hydrolysing sulfate-containing salts
• • C—CHEMISTRY; METALLURGY
  • C22—METALLURGY; FERROUS OR NON-FERROUS ALLOYS; TREATMENT OF ALLOYS OR NON-FERROUS METALS
  • C22B—PRODUCTION AND REFINING OF METALS; PRETREATMENT OF RAW MATERIALS
  • C22B3/00—Extraction of metal compounds from ores or concentrates by wet processes
  • C22B3/20—Treatment or purification of solutions, e.g. obtained by leaching
  • C22B3/22—Treatment or purification of solutions, e.g. obtained by leaching by physical processes, e.g. by filtration, by magnetic means, or by thermal decomposition
• • C—CHEMISTRY; METALLURGY
  • C22—METALLURGY; FERROUS OR NON-FERROUS ALLOYS; TREATMENT OF ALLOYS OR NON-FERROUS METALS
  • C22B—PRODUCTION AND REFINING OF METALS; PRETREATMENT OF RAW MATERIALS
  • C22B3/00—Extraction of metal compounds from ores or concentrates by wet processes
  • C22B3/20—Treatment or purification of solutions, e.g. obtained by leaching
  • C22B3/44—Treatment or purification of solutions, e.g. obtained by leaching by chemical processes
• • C—CHEMISTRY; METALLURGY
  • C22—METALLURGY; FERROUS OR NON-FERROUS ALLOYS; TREATMENT OF ALLOYS OR NON-FERROUS METALS
  • C22B—PRODUCTION AND REFINING OF METALS; PRETREATMENT OF RAW MATERIALS
  • C22B34/00—Obtaining refractory metals
  • C22B34/10—Obtaining titanium, zirconium or hafnium
  • C22B34/12—Obtaining titanium or titanium compounds from ores or scrap by metallurgical processing; preparation of titanium compounds from other titanium compounds see C01G23/00 - C01G23/08
  • C22B34/1236—Obtaining titanium or titanium compounds from ores or scrap by metallurgical processing; preparation of titanium compounds from other titanium compounds see C01G23/00 - C01G23/08 obtaining titanium or titanium compounds from ores or scrap by wet processes, e.g. by leaching
  • C22B34/124—Obtaining titanium or titanium compounds from ores or scrap by metallurgical processing; preparation of titanium compounds from other titanium compounds see C01G23/00 - C01G23/08 obtaining titanium or titanium compounds from ores or scrap by wet processes, e.g. by leaching using acidic solutions or liquors
  • C22B34/125—Obtaining titanium or titanium compounds from ores or scrap by metallurgical processing; preparation of titanium compounds from other titanium compounds see C01G23/00 - C01G23/08 obtaining titanium or titanium compounds from ores or scrap by wet processes, e.g. by leaching using acidic solutions or liquors containing a sulfur ion as active agent
• • C—CHEMISTRY; METALLURGY
  • C22—METALLURGY; FERROUS OR NON-FERROUS ALLOYS; TREATMENT OF ALLOYS OR NON-FERROUS METALS
  • C22B—PRODUCTION AND REFINING OF METALS; PRETREATMENT OF RAW MATERIALS
  • C22B34/00—Obtaining refractory metals
  • C22B34/10—Obtaining titanium, zirconium or hafnium
  • C22B34/12—Obtaining titanium or titanium compounds from ores or scrap by metallurgical processing; preparation of titanium compounds from other titanium compounds see C01G23/00 - C01G23/08
  • C22B34/1236—Obtaining titanium or titanium compounds from ores or scrap by metallurgical processing; preparation of titanium compounds from other titanium compounds see C01G23/00 - C01G23/08 obtaining titanium or titanium compounds from ores or scrap by wet processes, e.g. by leaching
  • C22B34/1259—Obtaining titanium or titanium compounds from ores or scrap by metallurgical processing; preparation of titanium compounds from other titanium compounds see C01G23/00 - C01G23/08 obtaining titanium or titanium compounds from ores or scrap by wet processes, e.g. by leaching treatment or purification of titanium containing solutions or liquors or slurries
• • Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
  • Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
  • Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
  • Y02P10/00—Technologies related to metal processing
  • Y02P10/20—Recycling

Definitions

• the present invention relates to a process for producing titania from a titaniferous material.
• titanium material is understood herein to mean any titanium-containing material, including by way of example ores, ore concentrates, and titaniferous slags .
• the present invention relates particularly to the sulfate process for producing titania from titaniferous material .
• the present invention provides a sulfate process for producing titania from a titaniferous material (such as ilmenite) of the type which includes the steps of:
• step (c) precipitating titanyl sulfate from the process solution from step (b) ;
• step (h) calcining the solid phase from step (g) and forming titania
• step (i) removing iron sulfate from the process solution from step (b) and/or the depleted process solution from step (d) .
• hydrated titanium oxides is understood herein to include, by way of example, compounds that have the formula TiO 2 .2H 2 O and TiO 2 -H 2 O.
• hydrated titanium oxides is understood herein to include compounds that are described in technical literature as titanium hydroxide (Ti(OH) 4 ) .
• concentrations of metals mentioned hereinafter are understood herein as being determined by ICP (all metals) or by titration (in the cases of Ti and Fe - ferrous and ferric) .
• the process includes supplying the separated process solution from step (d) and/or the separated liquid phase from step (g) to leach step (a) .
• the present invention is based on features of the step (c) of precipitating titanyl sulfate that are described hereinafter that were identified in the further research work.
• the acid concentration in the process solution containing dissolved titanyl sulfate from step (a) is at least 600 g/L, more preferably at least 650 g/L in order to precipitate titanyl sulfate in step (c) .
• the acid concentration may be controlled by one or more of the options of adding fresh acid to the process solution and/or removing water from the process solution, for example by evaporation and/or precipitation of one or more components of the process solution (such as iron sulfate) .
• the acidity of the process solution be controlled to be less than 750 g/L to minimise the possibility of undesirable co-precipitation of iron/titanium salts with titanyl sulfate in step (c) .
• Titanyl sulfate precipitation step (c) may be carried out on a continuous basis in a single reactor or in a plurality of reactors in series and/or in parallel.
• Step (c) may also be carried out on a batch basis in a single reactor or in a plurality of reactors.
• the reactor or reactors include (i) a vertically extending open-ended draft tube that divides the or each reactor into an inner chamber (defined by the draft tube) and an outer chamber and (ii) a stirring means in the tank.
• step (c) includes supplying process solution containing dissolved titanyl sulfate from steps (a) and/or (i) to the draft tube reactor or reactors and circulating the process solution successively through the draft tube and the outer chamber of the reactor or reactors for a sufficient period of time to allow precipitation of titanyl sulfate from solution in the process solution.
• Adjustment of the concentration of acid in the process solution from step (a) may be made either prior to or after addition of the process solution to the reactor or reactors.
• Step (c) may be carried out on a continuous basis.
• step (c) may include supplying process solution to the reactor or reactors on a continuous basis and discharging process solution containing suspended precipitated titanyl sulfate from the reactor or reactors on a continuous basis.
• Step (c) may also be carried out on a batch basis.
• step (c) may include filling the reactor or reactors with process solution, circulating process solution within the reactor or reactors, partially or completely discharging process solution containing suspended precipitated titanyl sulfate from the reactor or reactors, and repeating the above steps.
• the temperature of the process solution during step (c) is at least 90 0 C.
• a preferred temperature is 110 0 C.
• the applicant has also found that in one embodiment it is preferable that there be a relatively low concentration of titanium ions in the process solution during step (c) .
• the titanium concentration is less than 25 g/L.
• the low concentration of titanium ions is important to keep the resulting slurry "fluid" during titanyl precipitation in step (c) and in subsequent downstream processing of the slurry.
• step (c) it is preferable to control the process so that there is less than 10 g/L difference between concentration of titanium ions in the process solution supplied to step (c) and process solution containing suspended precipitated titanyl sulfate discharged from step (c) .
• titanyl sulfate precipitation is essentially self-seeded by virtue of precipitated titanyl sulfate circulating within the reactor or reactors.
• Seed may be added to the reactor or reactors as fresh seed and/or as recycled seed.
• the solids loading in process solution containing suspended precipitated titanyl sulfate discharged from step (c) be less than 10% solids by weight, more preferably 3-4% solids by weight.
• the precipitated titanyl sulfate is typically in the form of 100 x 1 micron needles that are difficult to handle and do not settle readily from the leach liquor. The applicant has found that there are significant materials handling issues with solids loadings greater than 10% solids by weight.
• the process of the present invention includes the following typical reactions. Leaching :
• Titanyl sulfate precipitation TiOSO 4 + 2H 2 O -> TiOSO 4 .2H 2 O
• the applicant has carried out experimental work on a laboratory scale and a pilot plant scale in relation to the above-described process.
• the flowsheet includes the following main steps:
• the leach step includes two leach stages 1 and 2 carried out in separate tanks 3, 5.
• Each leach stage is carried out in a single tank 3, 5 as indicated in the flowsheet or in multiple tanks (not shown) arranged in series .
• the leach stages 1 and 2 may be a fully counter- current or may be co-current with fresh return filtrate and/or wash filtrates being added to both leach stages.
• the chemistry of the leach step is:
• Leaching is carried out at a controlled acidity of 450 g/L ( ⁇ 25 g/L) H 2 SO 4 in each stage. Under these conditions about 80% leaching takes place in two leach stages, each of about 12 hours residence time.
• the leaching temperature is typically HO 0 C in each stage, which is less than the solution boiling point.
• the temperature is not controlled, but sufficient heat is generated during leaching to keep the slurry at about 110 0 C. Some top-up steam may be required for start up.
• One option is to use scrap iron addition into the leach tanks 3, 5. This has been found to increase leach kinetics significantly. Some reductant is required to convert ferric sulfate to ferrous sulfate to allow all iron to exit in the form of FeS ⁇ 4 crystals.
• the leach tanks 3, 5 are simple stirred tanks, each of which operates with an overflow to a thickener 7.
• Fibre-reinforced plastic (FRP) is suitable for wetted parts.
• Other suitable materials are acid bricks and tiles .
• the leach tanks 3, 5 are operated with gentle stirring so that the residence time of solids in the tanks is longer than the residence time of liquor in the tanks.
• the leach slurries discharged from the tanks 3, 5 are thickened in conventional thickeners 7.
• the settling rate is high for partly reacted ilmenite. Flocculation is possible. Underflow densities exceeding 60% are feasible, but lower solids loadings may be required to ensure pumpability.
• the solids loading in the leach step is controlled to give a process solution of about 40 g/L Ti, 90-100 g/L Fe and 400-450 g/L acid that leaves the leach step as overflow from the downstream thickener 7. These are the preferred concentrations of Fe and Ti without having ferrous sulfate or titanyl sulfate crystallise out prematurely .
• Ilmenite is added dry to the first leach tank 3.
• Thickener underflow from the thickener 7 of the first leach stage is pumped to the leach tank 5 of the second leach stage.
• Some recycled acid at about 350 g/L ( ⁇ 25 g/L) H 2 SO 4 which is a filtrate from a filtration step 37 downstream of a hydrolysis step 25 described hereinafter, is also pumped via line 11 to the leach tank 5.
• Titanyl sulfate crystallisation filtrate produced in a filtration step 31 described hereinafter is also added via line 11 to the second tank 5 to maintain the acidity at 450 g/L ( ⁇ 25 g/L) .
• Leaching is about 50-60% in the first stage rising to about 80% overall by the end of the second stage. Higher extractions are feasible with further leaching.
• the second stage leach slurry that is discharged from the leach tank 5 is thickened in the thickener 7.
• Second stage leach residue is filtered via filter lS and the resilient filter cake is suspended in recycled water. Limestone and lime are added to raise the pH to 7- 8, and the slurry is pumped to tailings 15.
• the process solution contained in the (unwashed) filter cake that is supplied to tailings 15 represents the major outlet for a number of minor elements, such as Cr and Zn.
• hot process solution discharged as the overflow from the downstream thickener 7 of the leach step is firstly cooled to about 6O 0 C in a heat exchanger (not shown) by heat exchange with process solution that has been discharged from a downstream crystallization tank (not shown) .
• the cooled pregnant process solution is then evaporatively cooled to about 20 0 C. This causes ferrous sulfate to crystallise out in the tank.
• the cooled process solution at this stage contains about 40 g/L Fe and 55 g/L Ti. The Ti concentration rises due to the lower volume of the cooled process solution.
• Removal of water by evaporation may be included to give a further water credit, allowing recovery of more weak acid.
• the ferrous sulfate crystals may be separated from the process solution by a conventional centrifuge (not shown) or by a belt filter (not shown) .
• the ferrous sulfate may be sold directly or converted to another saleable product.
• Mn, Al and Mg are minor elements which exit the circuit primarily with the ferrous sulfate crystals.
• the cold process solution that is discharged from the ferrous sulfate crystallization step 17 is partially reheated by cross flow heat exchanging against incoming hot process solution supplied to the step 17.
• the acid causes titanium to precipitate out of the process solution as titanyl sulfate dihydrate, TiSO 4 .2H 2 O, and form a slurry in accordance with the following reaction:
• the preferred operating temperature in the titanyl sulfate precipitation step is HO 0 C. Precipitation is very slow at less than 90 0 C.
• Precipitation is self seeding - the kinetics of crystallisation are accelerated by the presence of the product crystals.
• the solids have a long needle- like shape
• the precipitation tank (or one or more than one of the precipitation tanks in situations where there are multiple tanks) has an upstanding draft tube that has an upper inlet and a lower outlet and the draft tube is located to divide the tank into an outer chamber and a central cylindrical chamber.
• the assembly also includes an impeller to help circulation of the slurry. The slurry flows through the draft tube and the outer chamber in the tank.
• the solids in the slurry that is discharged from the precipitation tank or tanks are separated from the slurry by filtration.
• Filtration may be by a belt filter 21 shown in the flowsheet. However, maintaining the temperature of the filtrate probably requires pressure filtration.
• Some washing of the solids in the filter cake on the filter 21 by recycled acid from the hydrolysis step described hereinafter may be carried out as this improves purity of the high strength Ti solution going to hydrolysis .
• the acid washed TiOSO 4 .2H 2 O filter cake is a stable solid product and offers a convenient breakpoint in the flowsheet.
• the filter cake may be stock-piled as indicated by the numeral 27.
• Temporary storage of the acid washed crystals offers useful buffer capacity, and makes the process more robust.
• the filtrate contains about 700 g/L H 2 SO 4
• the acid washed filter cake from the stockpile 27 is re-pulped in a 30% H 2 SO 4 solution in a re-pulping step 29 and is then is pumped to a filter 31.
• the resultant slurry has an acid concentration of the order of 400 g/L.
• the filter cake on the filter 31 may be washed with hydrolysis filtrate to remove remaining entrained leach liquor.
• these washing steps may be applied to the initial filtration step to eliminate the need to re-pulp and re- filter the solids. However, in doing so the ability to store an intermediate filter cake is lost and the process is less robust.
• the water washed filter cake discharged from the filter 31 is added to a stirred tank 35. Over a period of about 2 hours at 6O 0 C the cake dissolves into a high strength Ti solution. Lower temperatures can also be used, although the dissolution time may be longer than 2 hours .
• Ti ⁇ 2 w Ti ⁇ 2 w . Concentrations exceeding 200 g/L Ti have been produced in laboratory and pilot plant work. However, 150 g/L or above is suitable for conventional pigment hydrolysis .
• the dissolution process preferably requires less than 100 g/L acid in the solution contained within the filter cake to ensure that the process goes to completion. If most or all acid is washed out the free acid content of the high strength solution is quite low.
• the acid to titania (A/T) ratio is usually about 1.3 (the theoretical minimum is 1.225 at zero acidity) .
• the product high strength solution produced in the stirred tank 35 is filtered through a filter cartridge (not shown) to remove siliceous and other fine particulate matter.
• the TiOSO 4 .2H 2 O in the filter cake does not immediately dissolve in water. Also its solubility in >20% H 2 SO 4 is quite low. This suggests the dissolution process is not strictly dissolution.
• the remarkable solubility of Ti at low acidity (>200 g/L Ti) compared to 20% H 2 SO 4 ( ⁇ 5 g/L Ti) favours this view.
• the filtered high strength Ti process solution is suitable for all conventional pigment hydrolysis processes.
• the pigment hydrolysis processes are typically batch processes due to critical need to control particle size. Feed solution to the pigment hydrolysis step is pretreated to generate about 2 g/L of Ti 3+ in the solution by conventional means .
• the Ti 3+ protects against oxidation of any iron to Fe 3+ , which coprecipitates with the Ti and imparts undesirable colour to the pigment.
• A/T ratio is a key process parameter.
• A/T ratio is:
• TiOSO 4 ] concentration is measured by a simple titration to pH 7 with sodium hydroxide solution, and the [TiO 2 ] g/L is Ti g/L ⁇ 0.6.
• the hydrolysis is carried out by preheating a heel of water, typically 10-20% of the volume of feed solution, to about 96 0 C.
• the process solution is also preheated to about 96 0 C and then is pumped across to the batch hydrolysis tank over a fixed time period.
• the hydrolysis tank 25 is equipped with steam heating and a gate type rake stirrer, which operates at low rpm.
• the steam heating is indirect so that the filtrate is not diluted by condensate.
• the initial few seconds of pumping cause the precipitation of very fine TiO(OH) 2 particles, which cause a milky aspect for about 30 seconds, then appear to redissolve.
• the fine particles are colloidal nuclei which control the size of both the resulting precipitate and the crystal size in the calciner discharge. Control of this step is therefore key to preparing good pigment.
• the slurry is then boiled for about 5 hours, by which time the Ti remaining in solution has been lowered to about 5 g/L.
• the slurry discharged from the hydrolysis tank 25 is filtered and washed with water on a belt filter 37 and produces a TiO(OH) 2 filter cake and a filtrate.
• the filtrate from the filter 37 contains 350-450 g/L H 2 S ⁇ 4 . This is returned via line 11 to the leach step for slurrying ilmenite and/or first stage thickener underflow.
• the acid units thereby are used to leach ilmenite. Recycling this acid is limited by the overall circuit water balance, and is favoured by higher acidity (ie. a lower volume equates to the higher acidity). Any excess is sent to a clean gypsum plant 49.
• rutile seed is made in a rutile seed preparation step 41 by reacting some TiO(OH) 2 filter cake discharged from the belt filter 37 with commercial 50% NaOH solution, for several hours at the boiling point (about 117° C) :
• the TiO(OH) 2 filter cake contains about 4% S in the form of absorbed basic titanium sulfates.
• the resulting sodium titanate is filtered and washed well to completely remove sulfate.
• the washed cake is then mixed with a carefully controlled amount of commercial 35% HCl to produce a solution of TiCl 4 ;
• the resulting slurry contains about 100 g/L TiO 2 in the rutile form. It may be used directly if the downstream flowsheet can tolerate Cl ions or it can be decantation washed to remove the NaCl .
• the Ti(OH) 2 filter cake that is discharged from the belt filter 37 and is not used to make rutile seed is re-pulped with clean H 2 SO 4 solution in a bleaching step 43.
• Al or Zn dust is added to reductively leach out chromophores such as Fe, Cr, Mn and V, which otherwise would reduce the whiteness of the final pigment.
• the bleach step typically takes place at 80° C.
• the rutile seed slurry is added at this point in a carefully controlled amount (e.g. 4.0+0.1 % w/w) .
• the bleached slurry is filtered and washed.
• the TiO(OH) 2 filter cake which has a sulfur content of about 2%, is mixed with a number of additives. These may be added as water solutions, or solids.
• the additives may include 0.2% K 2 O as K 2 SO 4 , 0.6% ZnO as ZnSO 4 and 0.3% P 2 O 5 as H 3 PO 4 .
• the additives control development of the rutile crystals during calcination, such that the crystal size is 0.27 ⁇ 0.03 ⁇ m, rutilisation is 98.5 ⁇ 0.5%, the crystals have a lenticular shape and are not sintered together.
• the process flowsheet also includes the steps of: calcination 45, finishing 47, and, if required, clean gypsum production 49. These steps are conventional steps.
• the process is able to produce coarse high purity titania that can be used, for example, as a feedstock for electrochemical reduction to produce titanium metal and alloys.
• Hydrolysis may be carried out continuously in this option. Several simple stirred tanks may be used in a cascade arrangement. Hydrolysis may be carried out at boiling point using steam heating, preferably indirect. Seeding is carried out by recycling thickener underflow to the first tank. This allows the slurry residence time to be 8-12 hours and generates a particle size d 50 of about 20 microns. Thickening gives a dense slurry of about 30% solids by weight, which may be vacuum filtered and washed. Bleaching may be carried out per the pigment process, if required. No rutile or chemical seeds are used. Calcination only requires a temperature of the order of 900 0 C for about 1 hour.
• This example describes a first stage of batch leaching.
• the filtrate contained 47 g/L Ti, 55 g/L Fe 2+ , 17 g/L Fe 3+ , 618 g/L free H 2 SO 4 , and had a specific gravity of 1.637 g/cm 3 .
• the weight of the washed filter cake was 39kg with a moisture content of 16.9%.
• the washed filter cake was assayed on a dry weight basis and was found to contain 15.3% FeO, 24.4% Fe 2 O 3 and 48.7% TiO 2 .
• This example describes a second stage of leaching using the first stage leach residue.
• a solution (273L) containing 3.6 g/L Ti, 6.1 g/L Fe 2+ , 2.4 g/L Fe 3+ , and 711 g/L free H 2 SO 4 was heated in a stirred, baffled vessel. Once the liquor had reached HO 0 C, 130 kg of wet cake prepared as described in Example 1, having a moisture content of 18.6% and containing 17.0% FeO, 22.7% Fe 2 O 3 and 49.4% TiO 2 , was introduced into the reaction vessel. Six 10 mm diameter mild steel rods were suspended in the reactor such that about 200 mm of the rods extended below the solution level. The mixture was allowed to react at HO 0 C for 3 hours, after which the temperature was allowed to fall steadily to 80 0 C over the next 3 hours.
• the resulting slurry was filtered through a recessed plate filter and the cake was washed with fresh water.
• the filtrate contained 46 g/L Ti, 38 g/L Fe 2+ , 20 g/L Fe 3+ , 513 g/L free H 2 SO 4 , and had a specific gravity of 1.553 g/cm 3 .
• the weight of the washed filter cake was 86 kg with a moisture content of 26.2%.
• the washed filter cake was assayed on a dry weight basis and was found to contain 13.3% FeO, 22.7% Fe 2 O 3 and 49.7% TiO 2 .
• This example describes the reduction and removal of Fe 3+ from the solution produced as described in Examples 1-2.
• a 5 L baffled glass reactor fitted with an 80 mm Rushton 6 turbine agitator was filled with 4 L of a solution containing 13.2 g/L Fe 3+ , 38.5 g/L Fe 2+ , 505 g/L free H 2 SO 4 and 40 g/L Ti.
• the agitation rate was set at 500 rpm.
• the reactor was temperature controlled to 50 0 C. On reaching this temperature a pump was used to recirculate the solution at 100 mL/min from the glass vessel, and through a 4 L fibre reinforced plastic (FRP) vessel containing a single 150 mm x 150 mm x 150 mm compressed bale of commercial detinned scrap steel.
• FRP fibre reinforced plastic
• the solution was introduced to the bottom of the FRP vessel and flowed up through the scrap and overflowed via gravity back into the glass reactor.
• the bale of scrap was height adjusted to be fully submerged below the level of the solution in the FRP vessel. After recirculating the solution for 45 min it was found that all Fe 3+ had been consumed. After 60 minutes the pump was turned off and the bale of scrap removed, whereupon it was found the solution contained 0 g/L Fe 3+ , 93 g/L Fe 2+ and 8.5 g/L Ti 3+ .
• ferrous sulfate may be batch precipitated from an ilmenite leach solution.
• titanyl sulfate dihydrate, TiOSO 4 .2H 2 O, crystals may be batch precipitated from an ilmenite leach solution prepared in the manner of Examples 1-2 by the addition of sulfuric acid, and that a high strength solution suitable for pigment manufacturing may be generated by dissolution of the crystals.
• Sulfuric acid (98%, 450 g) was mixed with an ilmenite leach solution (1500 mL) containing 440 g/L free H 2 SO 4 , 35.4 g/L Fe 2+ , 7.4 g/L Fe 3+ and 29 g/L Ti in a glass reactor equipped with baffles and a Teflon agitator.
• the resulting solution was heated to 110° C and titanyl sulfate crystals (4 g) were added as seed material.
• the mixture was stirred at this temperature for a total of 6 hours, during which a thick precipitate formed.
• the slurry was filtered and the cake was washed with water to give a wet filter cake (238 g) .
• the filtrate contained 16 g/L Ti, 638 g/L H 2 SO 4 and 48 g/L Fe, of which 6.6 g/L was as Fe 3+ .
• the filter cake dissolved after 3 hours to produce a titanyl sulfate solution containing 160 g/L Ti and 8.3 g/L Fe.
• This example describes the continuous precipitation of titanyl sulfate dihydrate, TiOSO 4 .2H 2 O, crystals, followed by vacuum filtration.
• Ilmenite leach solution (603.6 L) prepared as described in Examples 1-2, containing 524.7 g/L free H 2 SO 4 , 14.5 g/L Fe 2+ , 4.3 g/L Fe 3+ and 41.2 g/L Ti was mixed in an agitated fibreglass reactor with titanyl sulfate filtrate (1043.2 L) containing 637.5 g/L free H 2 SO 4 , 44.7 g/L Fe 2+ , 12.8 g/L Fe 3+ and 6.1 g/L Ti. Sulfuric acid (98%, 88.3 L) was then added along with titanyl sulfate filter cake (10 kg, 14% w/w solids) and the temperature was raised to HO 0 C.
• the reactor was 1.35 m diameter, with 1.3 m solution depth and contained a draft tube to improve mixing and the uniformity of mixing inside the reactor with minimal power input.
• the draft tube was 0.9 m internal diameter, 0.87 m high and raised 0.25 m from the bottom of the reactor.
• the reactor was fitted with an axial turbine with diameter of 0.6 m and raised 0.5 m from the floor of the reactor. The turbine operated at 250 rpm.
• the reactor was allowed to stir at temperature for 12 hours and a sample was taken and filtered.
• the titanium concentration in the liquor had dropped from an initial combined level of 17.3 g/L to 9.0 g/L.
• the feed and product pumps were started and set to flowrates of 4.6 L/min to allow for a 4.9 hour residence time with a constant combined feed solution containing 17.5 g/L Ti and 660 g/L H 2 SO 4 .
• the precipitator was run continuously this way for 10 hours producing 2742 L of titanyl sulfate slurry.
• Regular samples were taken from the reactor and filtered and analysed. These filtrate samples gave average concentrations of 7.5 g/L Ti and 611.8 g/L H 2 SO 4 .
• the precipitated titanyl sulfate dihydrate (TiOSO 4 .2H 2 O) was separated from the slurry using a belt filter, giving approximately 780 kg of filter cake with solids loading 14% w/w.
• titanyl sulfate dihydrate, TiOSO 4 .2H 2 O, crystals prepared in the manner of Examples 5 and 6 may be dissolved in water to produce a high strength solution.
• Titanyl sulfate dihydrate filter cake (19 kg) produced using the process described in Example 6 was re- pulped into a pumpable slurry using a solution containing 400 g/L H 2 SO 4 (4 L) mixed with re-pulp filtrate (36 L) containing 485 g/L free H 2 SO 4 , 6.7 g/L Fe 2+ , 9.6 g/L Fe 3+ and 5.9 g/L Ti. The slurry was allowed to stir for 15 minutes and then was filtered using a plate and frame filter.
• a sample of the filtrate from this filtering step was analysed and was found to contain 510 g/L free H 2 SO 4 , 8.9 g/L Fe 2+ , 10.7 g/L Fe 3+ and 7.4 g/L Ti.
• Water (50 L) was pumped through the filter to wash the solids.
• a sample of the filtrate from the washing step was analysed and found to contain 137 g/L free H 2 SO 4 , 2.2 g/L Fe 2+ , 3 g/L Fe 3+ and 3.3 g/L Ti.
• the washed solids were collected and were allowed to dissolve overnight.
• the resulting titanyl sulfate solution was filtered to remove fine, undissolved solids, which were predominately silica.
• the solution was found by assay to contain 467 g/L total H 2 SO 4 , 1.7 g/L Fe 2+ , 6.5 g/L Fe 3+ and 194 g/L Ti.
• This example describes the conversion of a titanyl sulfate dihydrate slurry directly into a high concentration titanium solution suitable for production of pigment, without an intermediate re-pulp step.
• Titanyl sulfate slurry (108 L) produced from the reactor described in Example 6 was filtered using a membrane pressure filter, instead of the belt filter described in Example 6.
• Recycled filter acid (45 L) containing 338.4 g/L free H 2 SO 4 , 10.1 g/L Fe 2+ , 2.3 g/L Fe 3+ and 10.1 g/L Ti was mixed with recycled wash water (50 L) containing 93.2 g/L free H 2 SO 4 , 3.4 g/L Fe 2+ , 0.7 g/L Fe 3+ and 3.4 g/L Ti and with 450 g/L sulfuric acid (10 L) .
• This mixed acid stream was then passed through the membrane pressure filter to wash the filtered solids.
• the solids were then further washed with water (50 L) and squeezed at a pressure of 4 bar for 5 minutes. Compressed air was then blown through the washed cake for 5 minutes . The filter cake was then removed from the filter and transferred to a container where it dissolved over a period of several hours to give a titanyl sulfate solution containing 218 g/L Ti and 333.5 g/L free H 2 SO 4 .
• This example describes the precipitation of pigment capable titanium hydroxide from high strength titanyl sulfate solution, using conventional practice.
• High strength titanyl sulfate solution (2.5 L) prepared as described in Example 7 was filtered to remove residual solids, then zinc dust (13 g) was added with stirring to remove ferric ions and to generate trivalent titanium.
• the solution on analysis was found to contain approximately 3.0 g/L of Ti 3+ .
• Concentrated sulfuric acid was added to give an A/T ratio of 1.70 ⁇ 0.05.
• the liquor was then concentrated by evaporation under reduced pressure to give a viscosity of 22-25 cp at 60° C and 330 + 10 g/L of TiO 2 in the final concentrated liquor.
• a water heel (0.5 L) was heated to 98 + 1°C in a glass reactor equipped with external electrical heating, a temperature controller, thermocouple and a rake type stirrer.
• the pretreated A/T controlled liquor (2.0 L) was separately heated to 98 + 1° C before being added to the water heel at a controlled rate such that all the liquor was added to the heel within 17 ⁇ 1 minutes.
• the temperature profile was then controlled to precipitate TiO 2 at a relative rate of 0.7 to 1.0% per minute by ramping the heating rate to give a temperature rise 0.5 0 C per min up to the boiling point. Agitation and heating were then stopped for 30 minutes.
• This example describes the production of rutile seed slurry, which may be used to assist with the rutilisation process during calcination.
• Titanium hydroxide filter cake (750 g, loss on ignition 68%) prepared as described in Example 9 was placed in a reaction vessel equipped with agitation and external heating. To the paste, pellets of sodium hydroxide (495 g) were slowly added over 30 minutes. A lid was then placed over the vessel. The temperature was set to 126°C and was maintained at this level with agitation for a further 60 minutes. At the end of this time the reaction was quenched to 60° C by adding sufficient water to lower the solids loading to 140 g/L equivalent TiO 2 (resulting in a total slurry volume of 1713 mli) . The slurry was then filtered using a Buchner funnel, and the precipitate washed with water at 60° C until the wash filtrate contained approximately 1 g/L equivalent Na 2 O, measured using a calibrated conductivity meter.
• the washed filter cake was then transferred to a reflux vessel equipped with an agitator and reslurried to 255 g/L equivalent TiO 2 (giving a slurry volume of 941 inL) .
• the slurry pH was adjusted to 2.8 using concentrated HCl (90 mL, 33% w/v) .
• a I g sample was removed to test for cake quality.
• To the remaining slurry sufficient concentrated HCl (298 mL, 33% w/v) was added to give an HCIrTiO 2 ratio of 0.41, and the temperature was raised to 60° C. The temperature was then increased to the boiling point at a controlled rate of 1° C per minute, and maintained at the boiling point for 90 minutes, after which the slurry was quenched with water to a volume of
• This example describes conventional reductive acid leaching of precipitated titanium hydroxide to remove chromophores .
• the filtered cake (63.5 g) from Example 9 was slurried in water (0.07 L) in a glass vessel equipped with a laboratory agitator. Concentrated H 2 S ⁇ 4 (98%, 9.0 g) was added to the stirred slurry after which coarse rutile nuclei (8.6 mL; prepared as described in Example 10) was added to the slurry to achieve 4% added rutile TiO 2 .
• the seeded slurry was made up to 0.1 L with water and heated to 75° C. Once at temperature zinc dust was added (0.5 g) and the slurry was maintained at temperature for 2 hours. The slurry was then cooled to 60° C and vacuum filtered in a Buchner funnel.
• This example describes calcination of titanium hydroxide to produce a substantially rutilised Ti ⁇ 2 calcine with crystal size suitable for pigment production.
• the cake paste (300 g) prepared as described in Example 11 was mechanically mixed in the presence of H3PO4 (98% solution), Al 2 (SO 4 ) 3 , K 2 SO 4 to give 0.15% P 2 O 5 , 0.18% Al 2 O 3 and 0.28% K 2 O as calculated after calcination, until a homogenous mixture is obtained.
• the paste was the extruded through a 5 mm die onto glass surface, covered then dried in a 75° C laboratory oven for 12 hours. The solids were then transferred to an electrically heated muffle furnace and the temperature was ramped to 920° C for 3 hours. The calcined solids were removed from the furnace and allowed to cool to ambient temperature, and the rutilisation measured by XRD was found to be 97.3%.
• Cooled TiO 2 solids (800 g) prepared as described in Example 12 were then processed through a laboratory hammer mill and sieved to achieved a particle size of less than 90 microns.
• the milled particles were then slurried in room temperature water to give a solids loading of 400 g/L (as TiO 2 ) with the aid of organic dispersant (1,1,1- tris-hydroxymethyl propane) .
• the dispersed slurry was pH adjusted to 10-11 by the addition of 10% w/v NaOH solution.
• the slurry was then passed through a hydraulic bead mill (bead size 0.8-1.0 mm, zirconia stabilized) in recirculation mode until a mean particle size of 0.27 ⁇ m was achieved.
• the slurry was then passed through a 325 ⁇ m sieve and the oversize was discarded.
• the sieved slurry (2 L) was then transferred to a 3 L beaker and heated to 50° C using an external electric heating mantle.
• the reagents were added at temperature such that a final concentration of Al 2 O 3 (3.5% of TiO 2 content) and ZrO 2 (0.88% of TiO 2 content) was achieved.
• the slurry was then filtered and washed with water at 60° C to achieve soluble salts in the cake as less than 0.1% as Na 2 SO 4 , and dried for about 3 hours under vacuum.
• the cake paste was then mechanically mixed in the presence of organic dispersant to achieve 0.2% carbon (w/w) on the TiO 2 .
• the paste was then extruded through a 5 mm die onto glass surface, which was covered and dried in a 75° C laboratory oven for 6 hours to achieve less than 1.0% H 2 O.
• the solids were then lightly hammer milled and the resulting solids passed through a laboratory air microniser which was operated at 6 bar (dried compressed air) for injection and grinding.
• the micronised product mean particle size was milled to between 0.30 and 0.33 ⁇ m as determined by optical density measurements .
• This example shows the ability to continuously hydrolyse high strength titanium solution to produce coarse TiO(OH) 2 which may be settled and filtered readily.
• a continuous pilot plant comprising of 2 x 5 L fibre-reinforced plastic (FRP) vessels, equipped with axial turbines and heaters, and an FRP thickener of diameter 30 cm and height 90 cm, equipped with rakes and a rake drive motor, was assembled.
• the FRP vessels and thickener were arranged in series with cascading overflow pipes between them to allow slurry to flow from vessel to vessel by gravity.
• An acidic slurry of titanium hydroxide (4 kg) prepared as described in Example 9 was placed in the first vessel as seed, and a solution of 300 g/L of H 2 SO 4 in water (5 L) was placed in the second vessel to assist the initial start up phase.
• the vessels were heated to a temperature of 100° C with stirring.
• Combined thickener underflow flowrate was 7 mL min (of which 5 mL/min was recycled as described) .
• Equilibrated thickener overflow flowrate was 9 mL/min.
• the solids loading in the thickener underflow reached 30% w/w by the end of the run.
• the particle size of the thickener underflow solids was determined using a Malvern 2000 laser sizer and was found to be d 50 7.8 ⁇ m.

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